CN1297336C - Active carbon fiber device and method for adsorbing, recovering and treating organic waste gas - Google Patents
Active carbon fiber device and method for adsorbing, recovering and treating organic waste gas Download PDFInfo
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- CN1297336C CN1297336C CNB2003101018396A CN200310101839A CN1297336C CN 1297336 C CN1297336 C CN 1297336C CN B2003101018396 A CNB2003101018396 A CN B2003101018396A CN 200310101839 A CN200310101839 A CN 200310101839A CN 1297336 C CN1297336 C CN 1297336C
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- 239000007789 gas Substances 0.000 title claims abstract description 121
- 238000000034 method Methods 0.000 title claims abstract description 43
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 229920000049 Carbon (fiber) Polymers 0.000 title claims description 31
- 239000004917 carbon fiber Substances 0.000 title claims description 31
- 239000010815 organic waste Substances 0.000 title abstract description 8
- 238000001179 sorption measurement Methods 0.000 claims abstract description 74
- 239000006096 absorbing agent Substances 0.000 claims abstract description 73
- 239000003960 organic solvent Substances 0.000 claims abstract description 36
- 238000001816 cooling Methods 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 21
- 238000007791 dehumidification Methods 0.000 claims abstract description 17
- 238000009826 distribution Methods 0.000 claims abstract description 7
- 239000002904 solvent Substances 0.000 claims abstract description 3
- 238000003795 desorption Methods 0.000 claims description 32
- 238000007084 catalytic combustion reaction Methods 0.000 claims description 30
- 238000004064 recycling Methods 0.000 claims description 30
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 28
- 239000002912 waste gas Substances 0.000 claims description 28
- 239000002250 absorbent Substances 0.000 claims description 26
- 230000002745 absorbent Effects 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 20
- 230000008676 import Effects 0.000 claims description 17
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 9
- 238000007599 discharging Methods 0.000 claims description 9
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 6
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 5
- 241000282326 Felis catus Species 0.000 claims description 3
- 150000001924 cycloalkanes Chemical class 0.000 claims description 3
- 239000008246 gaseous mixture Substances 0.000 claims description 3
- 239000003973 paint Substances 0.000 claims description 3
- 238000009941 weaving Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract 1
- 238000010521 absorption reaction Methods 0.000 description 21
- 230000000694 effects Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 7
- 231100000719 pollutant Toxicity 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000003610 charcoal Substances 0.000 description 4
- 239000000835 fiber Substances 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- 239000012298 atmosphere Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 208000002925 dental caries Diseases 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007306 turnover Effects 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000002657 fibrous material Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
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- 230000000149 penetrating effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The present invention relates to a device and a method for the recovery processing of organic pollution substances in exhaust air by activated carbon fiber. The device of the present invention, which uses activated carbon fiber for the recovery processing of organic waste gas is characterized in that the device used for the recovery processing of organic waste gas also comprises a rectification recovery system used for recovering organic solvent in the organic waste gas, and the rectification recovery system of the organic solvent comprises a rectifying tower which is arranged between an analyzed gas outlet and a condenser as well as a solvent receiving slot which is arranged behind the condenser; the device used for the recovery processing of organic waste gas can also comprises an analyzed gas bypass cooling system and can be additionally provided with a gas distribution baffle. The method for the recovery processing of organic waste gas of the present invention comprises: two or three absorbers are connected in series and are alternately used for the single-stage adsorption, the analysis, the cooling and the dehumidification, and totally uninterrupted recovery processing of the organic waste gas is realized by the connection and the distribution of pipelines and valves.
Description
Technical field
The present invention relates to a kind of apparatus and method with the organic pollution materials in the NACF recycling waste gas.Use the high-temperature water vapor desorb more specifically to a kind of then with the volatile organic contaminant in the carbon fiber adsorption and catalytic combustion waste gas, be condensed into the apparatus and method of recycling of a kind of organic exhaust gas of liquid organic solvent again with cooler.
Background technology
Organic exhaust gas means the gas that evaporate into the organic solvent class material in the atmosphere in petrochemical industry, electronics, the production of weaving, spray paint, as benzene, toluene, styrene, acetone, chloralkane, cycloalkane, n-hexane, ether etc.
The main method of handling such waste gas at present is absorption.Adsorbent has two kinds of granular activated carbon and NACFs.To have adsorption capacity big because NACF is compared with granular activated carbon; absorption, desorption rate is fast; the desorption efficiency height; the organic solvent impurity that reclaims is few; advantages such as long service life; the scope of application of NACF has now become the dominant technology of cleaning organic waste gas considerably beyond granular activated carbon.
As Fig. 5 of back, shown in Figure 6, the process of NACF recycling organic exhaust gas is: at normal temperatures and pressures, waste gas enters from a side of activated carbon fiber material layer, pass the NACF layer, organic pollution in the waste gas is adsorbed through the NACF layer time and is retained down, and cleaned air passes is discharged from opposite side.After the adsorbance of NACF acquired a certain degree, pollutant began to penetrate the NACF layer.Continuous increase along with the carbon fiber adsorption and catalytic combustion amount, the concentration of outlet pollutant also improves thereupon, when outlet pollutant levels during near the highest permission discharge standard, stops absorption, begin to use water vapor desorption, the organic gas of separating sucking-off reclaims after cooler is condensed into liquid.
The equipment of the organic exhaust gas of carbon fiber adsorption and catalytic combustion recovery at present mainly contains 4 kinds:
1. Japanese Toyo Boseki K.K is the absorber of cube shaped in the outward appearance of the exploitation seventies, and technology is divided two the casees and three casees two kinds of flow processs.Two casees flow processs be adsorb for one the case, another case carries out desorb, two the casees alternate cycles is used; Three casees flow processs are to adsorb for one the case, and another case carries out desorb, lower the temperature for the 3rd the case, and three case alternate cycles are used.Cooling method adopts the discharging air-blowing of adsorption box to take off in the interior carbon fiber adsorption and catalytic combustion core of cooling box and the residual water steam in the casing, makes the temperature in the absorber reduce to normal temperature.
2. patent CN2265880Y disclosed " big air quantity waste gas pollution control and treatment adsorption tower ".It is characterized by multitower use in parallel, a plurality of carbon fiber adsorption and catalytic combustion cores are housed in every tower, its purpose reduces gas by resistance for increasing the absorption surface of NACF, and the waste gas throughput on the minimizing unit are makes it reach an adsorption effect preferably.]
3. the disclosed low-concentration organic exhaust gas of patent CN2369746Y adsorbs and desorption apparatus.It is characterized by: the terminal valve of waste gas and desorb vapour all is connected on the total valve rod, realizes the mutual switching of the adsorption and desorption process of absorber by moving up and down of total valve rod, has simplified the control system that the adsorption and desorption process is switched mutually.
4. patent CN2320315Y discloses a kind of rotary type active charcoal fiber organic solvent separator.It is characterized by: the absorber shell is a cylinder, in a plurality of mutually isolated carbon fiber adsorption and catalytic combustion posts are housed, they rotate around the circle core shaft of absorber simultaneously, the import and export of waste gas and high temperature stripping gas are housed on the fixed position, two ends of absorber, when absorbent core went to the position of stripping gas, this core just was in desorption state.This device has mainly overcome many casees absorber necessary problem that relies on more Self controlling valve in the switching of adsorption and desorption.
Subject matter and weak point that above-mentioned various activated carbon fiber absorber exists are:
1. organic steam after the desorb and water vapour all directly enter cooler, carry out condensation after layering separate to be reclaimed by same temperature, to water can not layering organic solvent then also to add thermal rectification again and separate.Usually need fall condensate temperature lower in order to improve the Recovery of Organic Solvent rate, and condensed water does not need low temperature, but because organic solvent and water vapour are all cooled off by a temperature, not only cause cooling agent energy consumption height, and the effect of Recovery of Organic Solvent is difficult for also guaranteeing.
2. the absorbent core after the desorb does not just begin to enter adsorbed state through abundant cooling, because in the starting stage NACF temperature inside very high (approaching the temperature of stripping vapor) of adsorbing, adsorption rate is very low, the organic pollution in the exhaust is dense.Along with the increase by exhausted air quantity, the heat of NACF inside is taken out of gradually, and temperature drops to normal temperature gradually, and it is normal that adsorption effect could recover.Temperature fall time generally accounts for 1/4～1/2 of whole adsorption process.Pollutant levels height in the gas of discharging from absorber in this time period, compliance rate are low.
3. waste gas does not spread facility after entering absorber, the part air-flow directly blows on the nearer carbon fiber adsorption and catalytic combustion core of air inlet, make that the gas speed on the Topically active charcoal fiber is excessive, cause that penetrating has in advance just appearred in indivedual positions when most NACFs also have very big absorption surplus, have to stop absorption for this reason, the beginning desorb causes problems such as adsorption rate is low, adsorption cycle weak point, desorb frequency height, the increase of exhaust-gas treatment cost.
4. the entrance location of stripping vapor is located at the top of absorbent core center cavity, and steam sprays down.Because the height of absorbent core center cavity is bigger, generally reach about 2 meters, therefore enter the distribution of gas inequality in the cavity, cause the desorption rate difference of the NACF of different parts.Because the steam majority that sprays into easily accumulates in the position, middle and upper part of absorbent core, make that the desorption rate of charcoal fiber of position, middle and upper part is fast, the desorption rate of position, middle and lower part is slow, causes that desorption time prolongs, steam consumption is big.
5. the exit position of desorption gas all is located at the middle and lower part or the bottom of absorber, is unfavorable for discharge, the emptying of desorption gas.Owing to the proportion of the organic steam of separating sucking-off is lighter, easily accumulate in the top of absorber, outlet can not be discharged naturally at following organic steam, therefore need more steam that it is carried secretly out, not only caused the waste of steam but also the organic solvent gas of separating sucking-off all can not have been discharged, in adsorption process next time, be attracted to again on the NACF, occupy effective adsorption capacity.
Summary of the invention
One of the object of the invention is in order to overcome the above-mentioned defective of box activated carbon fiber absorber, to propose a kind of device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas.
The device of a kind of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas of one of the present invention is achieved in that
The device of a kind of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas of the present invention mainly comprises absorber, condenser; Described absorber comprises the absorbent core of being made up of the NACF layer that is positioned at its middle part, be positioned at the adsorption zone and the exhaust gas inlet of its underpart, be positioned at the exhaust area and the waste gas outlet on its top, also comprise stripping gas outlet and desorb steam inlet, it is characterized in that: the device of described recycling organic exhaust gas also comprises a rectifying recovery system that is used to reclaim organic solvent wherein, and the rectifying recovery system of described organic solvent comprises rectifying column between stripping gas outlet and condenser and the solvent receiving slit after the condenser.
The device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas of the present invention can also comprise a stripping gas bypass cooling system, promptly to the stripping vapor inlet line, draw a cooling bypass, be communicated with condenser, condensed water receiving slit, circulation coolant pump successively at the stripping gas outlet line that connects described stripping gas outlet and rectifying column.
In concrete enforcement, the device for carbon fiber adsorption and catalytic combustion recycling organic exhaust gas of the present invention can also add a distribution of gas baffle plate between the air inlet of adsorption zone and the absorbent core in described absorber; Described baffle plate profile is square, circular, an oval-shaped flat board, preferably square, the percent opening of described baffle plate is 0～50%, preferred 30%～40%, the area of described baffle plate is 1/3～3/4 of an adsorption box air inlet side area, preferred 2/3, its centre is relative with the center of air inlet.
In concrete enforcement, described desorption gas outlet can be arranged on the top board of adsorption zone, promptly on the dividing plate of adsorption zone and exhaust area; Can be provided with 1～8 in each adsorption box, preferred 4～6 desorption gas outlet, each desorption gas outlet is linked respectively on the total air escape pipe of desorption gas outlet again.
In concrete enforcement, the position of described stripping vapor import can be arranged on relative absorbent core 1/3～2/3, in preferred 1/2 altitude range.
In the time of concrete enforcement, carbon fiber adsorption and catalytic combustion device case body of the present invention can be cube, cylinder or other form.In the shell vertically lowering the carbon fiber adsorption and catalytic combustion core of 1～12 hollow cylinder, square column type or other shape is arranged.The absorbent core cavity bottom is shut, and open top opens and closes with valve control.
Two of the object of the invention provides a kind of method of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas.
The method of the present invention's two carbon fiber adsorption and catalytic combustion recycling organic exhaust gas is achieved in that
Organic exhaust gas of the present invention is included in petrochemical industry, electronics, the gas of the organic solvent material of discharging in producing of weaving, spray paint, described organic solvent material comprises benzene, toluene, styrene, acetone, chloralkane, cycloalkane, n-hexane, ether etc., the step of described method comprises
(1) adsorption process: described organic exhaust gas is by behind the absorber, and organic solvent material wherein is attracted on the absorbent core of being made up of the NACF layer, and is approaching or reach the highest permission discharge standard up to waiting to discharge in the gas organic concentration;
(2) desorption process: with the organic solvent material has been adsorbed in the stripping vapor blowback in a large number in process (1) absorbent core, stripping vapor passes the NACF layer from the inner surface of absorbent core, together discharges from the stripping gas outlet with the organic gas of separating sucking-off;
(3) rectification-recovery process: the stripping gas through process (2) enters rectifying column, reclaims organic solvent through condenser condenses again by cat head afterwards, and condensed water is discharged from rectifying Tata still.
(4) cool-down dehumidification process: promptly from the gaseous mixture of stripping gas the outlet steam of discharging and a part of organic gas of separating sucking-off before entering rectifying column, obtain being back to the stripping vapor import after the cooling through condenser, condensed water receiving slit, circulation cooling blower successively by a bypass.
The method of recycling organic exhaust gas of the present invention, can adopt two or three absorbers (4) series connection absorption, after single-stage desorb one cool-down dehumidification that hockets, and arrange by the connection of pipe valve, realize overall continual recycling organic exhaust gas process.
Advantage of the present invention is:
1. the gas of separating sucking-off is directly advanced rectifying column and utilize self heat to separate, the desorb rate of recovery improves 8～12% than directly reclaiming through the cooler condensation.Also can effectively utilize heat simultaneously, the disposable higher water-miscible organic solvent of purity that reclaims out.This recovery technology has been saved the elder generation in the traditional handicraft with the direct condensation of desorb gaseous mixture, reclaims the mixed liquor of organic solvent and water, and then adds the trouble of thermal release, has not only reduced energy consumption but also simplified technology.
2. owing to increased the absorber after the desorb is carried out extracorporal circulatory system cooling, dehumidification treatments, the problem that avoided that absorber is poor at the adsorption effect of high temperature absorption phase, the pollutant levels in the exhaust exceeds standard has improved 3～8% the organic solvent rate of recovery simultaneously.
3. by increasing baffle plate, improved the uniformity coefficient that passes each the position NACF layer gas speed in the absorber, total effective adsorption capacity of overall activity charcoal fiber is improved.Under the situation that pollutant levels are identical in NACF weight, intake velocity, exhaust, the adsorption capacity of NACF has increased by 2～10%.And because the increase of the adsorption capacity of NACF has prolonged adsorption cycle, the desorb number of times is reduced, can improve 5～15% the service life of NACF.
4. by improving the outlet position of desorption gas, reduce the residual quantity of organic solvent gas in the adsorption box, avoided the absorption that repeats of residue, improved the effective rate of utilization of absorber.
5. by improving the position of stripping vapor import, improve the even distribution of stripping vapor on NACF, make the effective rate of utilization of steam improve 10～15%.
Description of drawings
Fig. 1 improves the box carbon fiber adsorption and catalytic combustion schematic diagram in back
Fig. 2 carbon fiber adsorption and catalytic combustion box structure schematic diagram
The alternately process flow diagram of single stage adsorption-desorb-cool-down dehumidification of two absorbers of Fig. 3
The circulation two-stage series connection absorption-single-stage desorb-cool-down dehumidification technological process of three absorbers of Fig. 4
Fig. 5 carbon fiber adsorption and catalytic combustion old process schematic diagram
The conventional carbon fiber adsorption and catalytic combustion box structure of Fig. 6 schematic diagram
The specific embodiment
As shown in Figure 1 and Figure 2:
After pending organic exhaust gas enters absorber 4, disperse the back to enter, pass behind the NACF layer waste gas outlet 7 discharges from absorbent core 3 cavity tops from absorbent core 3 outer surfaces through distribution of gas baffle plate 2.The waste gas outlet 7 of closing absorbent core 3 tops after absorption finishes is opened the stripping vapor valve, and stripping vapor enters down from stripping vapor import 6 directions of the middle part of absorbent core 3 cavitys.Steam passes the NACF layer from the inner surface of absorbent core 3 then, together discharge through stripping gas outlet 8 with the organic gas of separating sucking-off from outer surface, go again rectifying column 9 utilize the heat of self separate organic solvent and water as the organic solvent boiling point that is recovered greater than 100 ℃ and water insoluble, just need not adopt rectifying column to separate, directly advance cooler condensation layering and get final product.Organic solvent steams from rectifying column 9 tops and obtains reclaiming after condenser 13 condensations, and the condensed water of tower still is discharged discharging after further handling.Steam off inlet valve, rectifying column 9 inlet valves after desorb is finished, ON cycle cooling blower 12, the high-temperature water vapor and the air of in the adsorption box and NACF inside are discharged, behind condenser 13 cool-down dehumidifications, again the gas of cooling is sent back in absorbent core 3 cavitys, cool-down dehumidification once more circulates, until the temperature in absorbent core and the absorber is reduced to 40～50 ℃, cooling blower 12 stops to circulate, close circulation cooling blower 12 terminal valves, open the waste gas terminal valve of adsorbed state, make absorber 4 be in the holding state of absorption.
This device both had been applicable to the alternately single stage adsorption-desorb-cool-down dehumidification technology of two absorbers, also was applicable to the circulation two-stage series connection absorption-single-stage desorb-cool-down dehumidification technology of three absorbers.
Accompanying drawing 3 is seen in the alternately technological process of single stage adsorption-desorb-cool-down dehumidification of two absorbers.Its technical process is: open the waste gas import and export valve of absorber 4A, close other valve, waste gas is discharging after absorber 4A handles.Wait to discharge in the gas organic concentration near or when reaching the highest permission discharge standard, close the waste gas import and export valve of absorber 4A, open the waste gas import and export valve of absorber 4B simultaneously, waste gas enters absorber 4B and begins absorption.Simultaneously, absorber 4A opens stripping vapor import and export valve, and absorber 4A is carried out desorb.Stripping gas reclaims organic solvent by overhead condenser 13 condensations after rectifying column 9 separates, condensed water is discharged from the tower still.After desorb is finished, steam off import and export valve, ON cycle cooling import and export valve, extract out with circulation cooling blower 12 remaining in the steam that reaches in the absorber 4A in the NACF layer after the desorb, send absorber again back to behind cooler 14 dehumidification by condensation, repeated multiple times is when treating that temperature drops to normal temperature in the absorber 4A, close circulation cooling blower 12 import and export valves, absorber 4A is stand-by.Treat in the discharging gas of absorber 4B organic concentration near or when reaching the highest permission discharge standard, open absorber 4A again and adsorb, absorber 4B carries out desorb equally by as above operation.Absorption-desorb the operation that hockets of two absorbers.
Accompanying drawing 4 is seen in the circulation two-stage series connection absorption-single-stage desorb-cool-down dehumidification technological process of three absorbers.Its technical process is: process gas at first enters absorber 4A and carries out one-level absorption, and the discharge gas of one-level absorption is sent into second class absorber 4P through the line pump pressurization, and the waste gas body after the secondary absorption enters atmosphere.When the gaseous contamination substrate concentration after the secondary absorption during near the highest permission concentration of emission of GB, switch by valve and to stop absorber 4A turnover waste gas, absorber 4B becomes one-level absorption simultaneously, absorber 4C is a secondary absorption.Begin absorber 4A is carried out desorb this moment.Desorption gas directly advances rectifying column 9 and separates organic solvent and water, and organic solvent reclaims through condenser 13 condensations from cat head, and condensed water is discharged from the tower still.Water vapour among the absorber 4A after the desorb and hot gas are extracted out by circulation cooling blower 12, send absorber 4A again back to after the cooling of cooler dehumidification by condensation, and repeated multiple times is till dropping to normal temperature with the temperature in the absorber 4A.Stop the cooling blower 12 that circulates then, switch valve, this moment, absorber 4A was in dormant state.When treating absorber 4C outlet pollutant levels near the highest permission concentration of emission of GB, switch by valve equally and stop absorber 4B turnover waste gas, absorber 4C becomes one-level absorption simultaneously, absorber 4A is a secondary absorption.Absorber 4B is carried out desorb, reclaim the organic solvent and the processing of lowering the temperature.Three absorber varying cyclically absorption positions, desorb is carried out in circulation, makes waste gas continuously carry out reclaiming clean.
Rigid condition: content of acetone 5000～8000mg/m in the waste gas
3, NACF consumption 150g, gas speed 0.5m
3/ h, 20～30 ℃ of adsorption temps.
| Absorber outlet acetone concentration, mg/m 3 | Maximal absorptive capacity, g/150g | |
| No baffle plate | Baffle plate is arranged | |
| 0 | 4.73 | 6.83 |
| 100 | 6.14 | 8.26 |
| 200 | 9.03 | 12.12 |
| 500 | 11.51 | 16.27 |
| 1000 | 14.63 | 21.35 |
Embodiment 2 n-hexane waste gas adsorption tests
Rigid condition: n-hexane content 3000～5000mg/m in the waste gas
3, NACF consumption 150g, gas speed 0.5m
3/ h, 20～30 ℃ of adsorption temps.
| Absorber outlet n-hexane concentration, mg/m 3 | Maximal absorptive capacity, g/150g | |
| No baffle plate | Baffle plate is arranged | |
| 0 | 3.51 | 5.82 |
| 100 | 6.02 | 7.94 |
| 200 | 9.61 | 12.83 |
| 500 | 12.28 | 17.31 |
| 1000 | 14.98 | 22.13 |
NACF consumption 150g, acetone adsorbance 20～22g, steam pressure 0.4～0.6Mpa (saturated vapor).
| Steam consumption Kg | Content of acetone in the absorber in the residual gas, mg/m 3 | |
| The bottom exhaust | Top vent | |
| 1 | 7000～10000 | 1300～1500 |
| 1.5 | 3000～5000 | 280～420 |
| 2 | 300～800 | 15～55 |
NACF consumption 150g, n-hexane adsorbance 21～23g, steam pressure 0.4～0.6Mpa (saturated vapor).
| Steam consumption Kg | N-hexane content in the absorber in the residual gas, mg/m 3 | |
| The bottom exhaust | Top vent | |
| 1 | 10000～15000 | 2200～3000 |
| 1.5 | 5000～8000 | 300～500 |
| 2 | 1300～3000 | 30～70 |
NACF consumption 150g, about acetone adsorbance 21g, stripping vapor pressure 0.4～0.6Mpa (saturated vapor).
Acetone yield (unit: g)
NACF consumption 150g, about acetone adsorbance 22g, stripping vapor pressure 0.4～0.6Mpa (saturated vapor).
N-hexane yield (unit: g)
Recovering condition: 140～160 ℃ of stripping vapor temperature;
Steam consumption 1.2Kg;
Reclaim liquid from 20～30 ℃ of the discharge temperatures of cooler
Claims (10)
1. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas, described device comprises absorber (4) and condenser (13); Described absorber (4) comprises the absorbent core of being made up of the NACF layer (3) that is positioned at its inside, be positioned at the adsorption zone (15) and the exhaust gas inlet (1) of its underpart, be positioned at the exhaust area (16) and the waste gas outlet (7) on its top, also comprise stripping vapor import (6) and stripping gas outlet (8), it is characterized in that:
The device of described recycling organic exhaust gas also comprises a rectifying recovery system that is used to reclaim organic solvent wherein, and the rectifying recovery system of described organic solvent comprises rectifying column (9) and condenser (13) the solvent receiving slit (10) afterwards that is positioned between stripping gas outlet (8) and the condenser (13).
2. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 1, it is characterized in that: the device of described recycling organic exhaust gas also comprises a stripping gas bypass cooling system, promptly to stripping vapor import (6) pipeline, draw a cooling bypass, be communicated with condenser (14), condensed water receiving slit (11), circulation cooling blower (12) successively at the stripping gas outlet line that connects described stripping gas outlet (8) and rectifying column (9).
3. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 1 or 2 is characterized in that:
In described absorber (4), also has a distribution of gas baffle plate (2) between the air inlet (1) of adsorption zone (15) and the absorbent core (3); The flat board that one of described baffle plate (2) is square for profile comprises, circular, oval, the percent opening of described baffle plate (2) is 0～50%, the area of described baffle plate (2) is 1/3～3/4 of an adsorption box air inlet side area, and the center of described baffle plate (2) is relative with the center of air inlet (1).
4. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 3, it is characterized in that: described baffle plate (2) is square flat board for profile, the percent opening of described baffle plate (2) is 30%～40%, and the area of described baffle plate (2) is 2/3 of an adsorption box air inlet side area.
5. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 1 or 2, it is characterized in that: described desorption gas outlet (8) is arranged on the top board of adsorption zone (15), promptly on the dividing plate of adsorption zone (15) and exhaust area (16); 1～8 desorption gas outlet (8) is set in each adsorption box, and each desorption gas outlet (8) is linked respectively on the total air escape pipe of desorption gas outlet (8) again.
6. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 1 or 2 is characterized in that:
The position of described stripping vapor import (6) is arranged in relative absorbent core 1/3～2/3 altitude range.
7. the device of carbon fiber adsorption and catalytic combustion recycling organic exhaust gas as claimed in claim 4, it is characterized in that: described desorption gas outlet (8) is arranged on the top board of adsorption zone (15), promptly on the dividing plate of adsorption zone (15) and exhaust area (16); 4～6 desorption gas outlets (8) are set in each adsorption box, and each desorption gas outlet (8) is linked respectively on the total air escape pipe of desorption gas outlet (8) again;
The position of described stripping vapor import (6) is arranged in relative absorbent core 1/2 altitude range.
8. the device of carbon fiber adsorption and catalytic combustion as claimed in claim 7 recycling organic exhaust gas is characterized in that: the device of described recycling organic exhaust gas is the circulation plural serial stage absorption-single-stage desorb-cool-down dehumidification device that comprises two or three absorbers (4).
9. the method for the device of use such as claim 7 or 8 described carbon fiber adsorption and catalytic combustion recycling organic exhaust gas, described organic exhaust gas is included in petrochemical industry, electronics, the gas of the organic solvent material of discharging in producing of weaving, spray paint, described organic solvent material comprises benzene, toluene, styrene, acetone, chloralkane, cycloalkane, n-hexane, ether, the step of described method comprises
(1) adsorption process: described organic exhaust gas is by behind the absorber (4), and organic solvent material wherein is attracted on the absorbent core of being made up of the NACF layer (3), and is approaching or reach the highest permission discharge standard up to waiting to discharge in the gas organic concentration;
(2) desorption process: the absorbent core (3) of in process (1), having adsorbed the organic solvent material with the stripping vapor blowback in a large number, stripping vapor passes the NACF layer from the inner surface of absorbent core, together discharges from stripping gas outlet (8) with the organic gas of separating sucking-off;
(3) rectification-recovery process: the stripping gas through process (2) enters rectifying column (9), reclaims organic solvent through condenser (14) condensation again by cat head afterwards, and condensed water is discharged from rectifying column (9) tower still.
(4) cool-down dehumidification process: promptly from the gaseous mixture of stripping gas outlet (8) steam of discharging and a part of organic gas of separating sucking-off in that to enter rectifying column (9) preceding, pass through condenser (14), condensed water receiving slit (11), circulation cooling blower (12) successively by a bypass and obtain being back to stripping vapor import (6) after the cooling.
10. the method for recycling organic exhaust gas as claimed in claim 9 is characterized in that:
The method of described recycling organic exhaust gas comprises with the single stage adsorption-desorb-cool-down dehumidification that hockets after the series connection of two or three absorbers (4), and the connection by pipe valve is arranged, and realizes overall continual recycling organic exhaust gas process.
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| CNB2003101018396A CN1297336C (en) | 2003-10-20 | 2003-10-20 | Active carbon fiber device and method for adsorbing, recovering and treating organic waste gas |
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| CNB2003101018396A CN1297336C (en) | 2003-10-20 | 2003-10-20 | Active carbon fiber device and method for adsorbing, recovering and treating organic waste gas |
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| CN1297336C true CN1297336C (en) | 2007-01-31 |
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